Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/44—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by addition reactions, i.e. reactions involving at least one carbon-to-carbon double or triple bond
  • C07C29/46—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by addition reactions, i.e. reactions involving at least one carbon-to-carbon double or triple bond by diene-synthesis
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
  • B01J23/44—Palladium

Definitions

• the present invention relates to a method for producing 2,7-octadien-1-ol, and particularly to a method for producing 2,7-octadien-1-ol by reacting butadiene with water in the presence of a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal.
• 2,7-Octadien-1-ol can be derived to 7-octenal by isomerization reaction, and 7-octenal can be derived to 1,9-nonanedial by hydroformylation reaction. Since the 1,9-nonanedial can be derived to 1,9-nonanediamine useful as a raw material for a polymer monomer by a reductive amination reaction, 2,7-octadien-1-ol has high industrial value, and development of a method for producing the same is also important.
• the main emphasis is placed on providing an industrially advantageous method for producing 2,7-octadien-1-ol in which an expensive palladium catalyst is highly efficiently recovered without deteriorating the stability of the palladium catalyst, the palladium catalyst is cyclically reused, and the reaction rate per palladium atom is improved.
• 2,6-octadien-1-ol is produced as a by-product in a non-negligible amount with the progress of the reaction.
• the production of 2,6-octadien-1-ol is not described or recognized in the above-mentioned prior art documents.
• 2,6-Octadien-1-ol has a boiling point close to that of 2,7-octadien-1-ol, which makes its separation difficult. This affects the quality of the desired product 2,7-octadien-1-ol. And in some applications, its presence has been found to cause problems.
• An object of the present invention is to provide an industrially advantageous method for producing 2,7-octadien-1-ol, which can improve the productivity of 2,7-octadien-1-ol while suppressing the production of 2,6-octadien-1-ol as a by-product.
• the present invention is as the following [1] to [11].
• the method for producing 2,7-octadien-1-ol of the present invention includes at least a step (1) of feeding a raw material mixture liquid containing butadiene, a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal, a tertiary phosphorus compound, an amine compound, and water to a telomerization reactor, and a step (2) of reacting butadiene and water in a carbon dioxide atmosphere in the telomerization reactor to obtain a reaction mixture liquid containing 2,7-octadien-1-ol, and if necessary, further includes other steps.
• the residence time of the raw material mixture liquid in the telomerization reactor is 1.3 to 3.0 hours.
• the present inventors have found that the amount of 2,6-octadien-1-ol produced can be reduced while increasing the productivity of 2,7-octadien-1-ol by controlling the residence time within the above range.
• the “residence time of the raw material mixture liquid” in the description herein is a so-called apparent residence time, and is calculated by “the amount of the reaction mixture liquid in the telomerization reactor ⁇ the feed amount of the raw material mixture liquid”.
• the “amount of the reaction mixture liquid in the telomerization reactor” means the “amount of the liquid remaining in the telomerization reactor”.
• the amount of the reaction mixture liquid in the telomerization reactor is not particularly limited, and is preferably 0.01 m 3 to 1,000 m 3 , more preferably 0.1 m 3 to 500 m 3 , and still more preferably 1 m 3 to 100 m 3 .
• the feed amount of the raw material mixture liquid is not particularly limited, and is preferably 0.003 m 3 /hour to 769 m 3 /hour, more preferably 0.03 m 3 /hour to 385 m 3 /hour, and still more preferably 0.3 m 3 /hour to 77 m 3 /hour.
• butadiene, a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal, a tertiary phosphorus compound, an amine compound, and water are used as essential components, and if necessary, an organic solvent and other components are used as optional components.
• butadiene any of industrially available hydrocarbon mixtures usually called C4 fractions in petrochemicals can be used, but since the palladium catalyst is poisoned by acetylene, sulfur, halogen, and the like, it is preferred to use butadiene having a content of these components of 0.1 ppm or less. Such butadiene is called a polymerization grade product or a chemical grade product, and is industrially available.
• the content of butadiene in the raw material mixture liquid fed to the telomerization reactor is not particularly limited, and is preferably 1% to 30% by mass, more preferably 3% to 25% by mass, and still more preferably 5% to 20% by mass, from the viewpoint of production efficiency and suppression of a decrease in reaction efficiency associated with two phase separation.
• Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal used in the production method of the present invention a compound containing a Group 6 to 11 transition metal in the long periodic table can be used.
• the Group 6 to 11 transition metal one or more selected from the group consisting of Group 6 transition metals and Group 10 transition metals are preferable, Group 10 transition metals are more preferable, and palladium is still more preferable.
• the compound containing a Group 6 to 11 transition metal include a molybdenum compound, a tungsten compound, a nickel compound, a palladium compound, and a platinum compound.
• a palladium compound is preferable.
• the palladium compound examples include divalent palladium complexes such as palladium acetate, palladium acetylacetonate, palladium chloride, and palladium nitrate; and 0-valent palladium complexes such as tris(dibenzylideneacetone)dipalladium, tetrakis(triphenylphosphine)palladium, and bis(1,5-cyclooctadiene)palladium.
• divalent palladium complexes such as palladium acetate, palladium acetylacetonate, palladium chloride, and palladium nitrate
• 0-valent palladium complexes such as tris(dibenzylideneacetone)dipalladium, tetrakis(triphenylphosphine)palladium, and bis(1,5-cyclooctadiene)palladium.
• One of these may be used alone, or two or more thereof may be used in
• one or more selected from the group consisting of palladium acetate, palladium chloride, and tris (dibenzylideneacetone)dipalladium are preferable, and palladium acetate is more preferable.
• the content of the Group 6 to 11 transition metal catalyst in the raw material mixture liquid to be fed to the telomerization reactor is not particularly limited, and is preferably 10 to 1,000 ppm by mass, more preferably 50 to 800 ppm by mass, and still more preferably 100 to 500 ppm by mass from the viewpoint of production efficiency and suppression of the amount of catalyst elution.
• the palladium concentration in the raw material mixture is preferably 450 to 650 ppm by mass, and more preferably 500 to 600 ppm by mass.
• a tertiary phosphorus compound as a ligand capable of forming a complex by coordinating to a Group 6 to 11 transition metal is used.
• phosphine, phosphite, phosphonite, or the like is preferable.
• tertiary phosphorus compound examples include aliphatic phosphines such as triisopropylphosphine, tri-n-butylphosphine, and tri-n-octylphosphine; alicyclic phosphines such as tricyclohexylphosphine; hydrophobic aromatic phosphines such as triphenylphosphine, tritolylphosphine, diphenyl-p-chlorophenylphosphine, and trimesitylphosphine; hydrophilic aromatic phosphines such as lithium 3-diphenylphosphinobenzenesulfonate, sodium 3-diphenylphosphinobenzenesulfonate, triethylamine 3-diphenylphosphinobenzenesulfonate, and tris(sodium 3-sulfophenyl)phosphine; phosphites such as triethyl phos
• an aromatic phosphine that is, at least one of a hydrophobic aromatic phosphine and a hydrophilic aromatic phosphine is preferable, a hydrophilic aromatic phosphine is more preferable, and at least one of lithium 3-diphenylphosphinobenzenesulfonate, triethylamine 3-diphenylphosphinobenzenesulfonate, and sodium 3-diphenylphosphinobenzenesulfonate is particularly preferable.
• the hydrophilic aromatic phosphine refers to an aromatic phosphine having a hydrophilic group, such as a group represented by —SO 3 M, —COOM (M represents an alkali metal ion or H + N(R 11 )(R 12 )(R 13 )), or N(R 14 )(R 15 ).
• R 11 , R 12 , and R 13 each independently represent a hydrogen atom or an alkyl group having 1 to 3 carbon atoms
• R 14 and R 15 each independently represent an alkyl group having 1 to 3 carbon atoms.
• the hydrophobic aromatic phosphine refers to an aromatic phosphine having no hydrophilic group.
• the amount of the tertiary phosphorus compound present in the raw material mixture liquid is not particularly limited, and can be determined in consideration of the ratio to the Group 6 to 11 transition metal contained in the Group 6 to 11 transition metal catalyst, preferably palladium atom.
• the content of the tertiary phosphorus compound in the raw material mixture liquid is preferably 0.1 to 100 mol times, more preferably 1 to 50 mol times, and still more preferably 5 to 30 mol times, with respect to the content of the Group 6 to 11 transition metal.
• a tertiary phosphorus compound preferably a hydrophilic aromatic phosphine
• the amount is 0.1 mol times or more, the formation of catalytically active species becomes sufficient, it is possible to suppress side reactions to vinylcyclohexene and the like, and thus to suppress a decrease in the yield of 2,7-octadien-1-ol, and it is also possible to suppress a decrease in the recovery rate of a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal, preferably a palladium catalyst.
• the amount is 100 mol times or less, the coordination of butadiene to the palladium catalyst is not inhibited, and the reaction rate can be maintained.
• M in the sulfonic acid group (—SO 3 M) contained in the hydrophilic aromatic phosphine may be an ammonium cation derived from the tertiary amine used in the reaction. Further, the sulfonic acid group (—SO 3 M) may be ionized into —SO 3 ⁇ and M + .
• the tertiary phosphorus compound coexists with an alkenyl compound such as 2,7-octadien-1-ol which is a product. Therefore, as described in JP 2002-371089 A and the like, the tertiary phosphorus compound (preferably hydrophilic aromatic phosphine) may form a phosphonium salt by reaction with 2,7-octadien-1-ol or the like.
• the content of the tertiary phosphorus compound in the raw material mixture liquid to be fed to the telomerization reactor is not particularly limited, and is preferably 0.1% to 30% by mass, more preferably 0.5% to 20% by mass, and still more preferably 1% to 10% by mass from the viewpoint of stabilization of the transition metal catalyst and suppression of precipitation of the tertiary phosphorus compound.
• the amine compound can react with water and carbon dioxide in the reaction system to produce an ammonium ion and a hydrogen carbonate ion.
• the hydrogen carbonate ion can produce 2,7-octadien-1-ol by attacking a reaction intermediate formed from one atom of a Group 6 to 11 transition metal contained in the Group 6 to 11 transition metal catalyst, preferably palladium, one molecule or two molecules of a tertiary phosphorus compound, two molecules of butadiene, and the like.
• the amine compound is not particularly limited, and may be an ammonium salt, but is preferably a tertiary amine, more preferably a monodentate tertiary amine having a basicity constant (pKa) of 7 or more, and examples thereof include trimethylamine, triethylamine, tri-n-butylamine, 1-N,N-dimethylamino-2-propanol, N,N-dimethyl-2-methoxyethylamine, N-methylmorpholine, and N,N,N′,N′-tetramethylhexamethylenediamine.
• trimethylamine and triethylamine are preferable in consideration of various points such as reaction performance, boiling point, solubility, and price.
• the mass ratio of the amine compound to water [amine compound/water] is preferably 0.1 to 10, and more preferably 0.5 to 5.
• this mass ratio is 0.1 or more, the hydrogen carbonate ion concentration in the reaction system becomes sufficiently high, so that the reaction rate is also increased, and at the same time, the by-production of 1,3,7-octatriene and vinylcyclohexene can be suppressed.
• this mass ratio is 10.0 or less, the coordination of the tertiary phosphorus compound to palladium is not likely to be inhibited, and as a result, the by-production of 1,3,7-octatriene and vinylcyclohexene can be suppressed.
• the content of the amine compound in the raw material mixture liquid to be fed to the telomerization reactor is not particularly limited, and is preferably 0.1% to 20% by mass, more preferably 1% to 15% by mass, and still more preferably 3% to 10% by mass, from the viewpoint of improving the reaction rate and ensuring the volume efficiency.
• the monodentate tertiary amine reacts with water and carbon dioxide in the reaction system and exists as an equilibrium mixture (carbonate and/or hydrogen carbonate) of (i) ammonium ions and (ii) carbonate ions and hydrogen carbonate ions, and the existing ratio of the carbonate and/or hydrogen carbonate of the amine compound under the reaction conditions depends on the reaction liquid temperature and the partial pressure of carbon dioxide. From the viewpoint of further improving the productivity of 2,7-octadien-1-ol, it is preferable to determine the amount of carbon dioxide using pressure or the like as an index.
• water having a purity that does not adversely affect the telomerization reaction is preferably used.
• water water having a purity that does not adversely affect the telomerization reaction is preferably used.
• industrially it is preferable to use ion-exchanged water or drain water obtained by condensing steam.
• the tertiary phosphorus compound forms a complex with a metal ion derived therefrom, so that the formation of the palladium catalyst becomes insufficient, and a side reaction to vinylcyclohexene or the like occurs, so that the yield of 2,7-octadien-1-ol decreases and the recovery rate of the palladium catalyst decreases.
• the content of water in the raw material mixture liquid to be fed to the telomerization reactor is not particularly limited, and is preferably 1% to 50% by mass, more preferably 5% to 40% by mass, and still more preferably 10% to 30% by mass, from the viewpoint of suppressing a decrease in the reaction rate and suppressing a decrease in the reaction efficiency due to two phase separation.
• the organic solvent used as an optional component as necessary is not particularly limited, and it is preferable that the organic solvent can be used in the presence of an organic solvent that can at least partially dissolve butadiene, a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal, a tertiary phosphorus compound, and an amine compound and does not adversely affect the telomerization reaction.
• solvents examples include ethers such as diethyl ether, tetrahydrofuran, and 1,4-dioxane; ketones such as acetone and methyl ethyl ketone; nitriles such as acetonitrile and benzonitrile; sulfones such as sulfolane and methylsulfolane; esters such as methyl acetate and ethyl acetate; aromatic hydrocarbons such as benzene, toluene, and xylene; and aliphatic hydrocarbons such as butane, hexane, and cyclohexane. One of these may be used alone, or two or more thereof may be used in combination.
• At least one selected from the group consisting of tetrahydrofuran, 1,4-dioxane, and sulfolane is preferable, and sulfolane is more preferable.
• Sulfolane is preferred because it is miscible with both butadiene and water, allows the separation of 2,7-octadien-1-ol by extraction from the reaction mixture liquid, and does not adversely affect the reaction even in long-term continuous use.
• the content of the organic solvent in the raw material mixture liquid to be fed to the telomerization reactor is not particularly limited, and is preferably 1% to 80% by mass, more preferably 20% to 70% by mass, and still more preferably 30% to 60% by mass, from the viewpoint of ensuring the volume efficiency and suppressing a decrease in the reaction efficiency due to two phase separation.
• a raw material mixture liquid containing butadiene, a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal, a tertiary phosphorus compound, an amine compound, and water is fed to a telomerization reactor (step (1)) and subjected to a telomerization reaction.
• butadiene and water are reacted under a carbon dioxide atmosphere in a telomerization reactor in the presence of a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal (preferably palladium) and a tertiary phosphorus compound (preferably a hydrophilic aromatic phosphine) (in a state where optional components such as an organic solvent are further present as necessary) to obtain a reaction mixture liquid containing 2,7-octadien-1-ol (step (2)).
• a Group 6 to 11 transition metal catalyst containing a Group 6 to 11 transition metal (preferably palladium) and a tertiary phosphorus compound (preferably a hydrophilic aromatic phosphine)
• the raw material mixture liquid is fed to the telomerization reactor includes not only a case where the raw material mixture liquid is prepared by mixing the raw materials in advance and then the raw material mixture liquid is fed to the telomerization reactor, but also a case where a part or all of the raw materials are fed to the telomerization reactor without being mixed in advance, and the former is preferable.
• the reaction can preferably be carried out using a complete mixing reactor.
• the reaction can be carried out in a batch system (including a semi-continuous system) or a continuous flow system, and can also be carried out in a continuous flow system by connecting two or three complete mixing reactors in series.
• the reaction is preferably carried out in a continuous flow system. That is, the step (1) and the step (2) in the production method of the present invention are preferably carried out not sequentially but simultaneously.
• completely mixing reactor refers to a reactor designed so that raw materials supplied into the reactor are mixed into a substantially uniformly dispersed state without a moment of time.
• the mass ratio of butadiene to 2,7-octadien-1-ol present in the telomerization reactor in a steady state can be appropriately set according to a desired butadiene conversion rate.
• the mass ratio of butadiene and 2,7-octadien-1-ol to water [(butadiene+2,7-octadien-1-ol)/water] present in the reaction system is preferably 0.1 to 50, and more preferably 0.5 to 10.
• Any carbon dioxide may be used as long as it is present as carbon dioxide in the reaction system, and for example, it can be supplied as molecular carbon dioxide, carbonic acid, a carbonate, or a bicarbonate, and it is preferable to use molecular carbon dioxide and perform the reaction under carbon dioxide pressure in order to increase the solubility of molecular carbon dioxide in the reaction system.
• the partial pressure of carbon dioxide is in a state of 0.05 MPa to 5 MPa (absolute pressure).
• reaction pressure of the entire reaction system and the vapor pressures of butadiene, the reaction product, and the solvent under the reaction temperature are also in the range of 0.101 MPa (normal pressure) to 9.8 MPa.
• a gas inert to the reaction such as nitrogen or argon, may be allowed to coexist.
• the telomerization reaction is preferably performed at a temperature (reaction liquid temperature) of 50° C. to 90° C. From the viewpoint of further improving the productivity of 2,7-octadien-1-ol, the telomerization reaction is more preferably performed at a temperature of 50° C. to 80° C., and still more preferably performed at a temperature of 65° C. to 75° C. That is, the temperature in the telomerization reactor is preferably 50° C. to 90° C., more preferably 50° C. to 80° C., and still more preferably 65° C. to 75° C.
• the method of the present invention is characterized in that the residence time of the raw material mixture liquid in the telomerization reactor is controlled to 1.3 to 3.0 hours.
• the residence time may also vary depending on the temperature of the reaction liquid, the amount of the Group 6 to 11 transition metal catalyst containing the Group 6 to 11 transition metal (preferably palladium) used as a catalyst, the amount of the tertiary phosphorus compound (preferably hydrophilic aromatic phosphine) used, the supply amount of butadiene, the amount of the amine compound used, the target conversion rate of butadiene, and the like, and is preferably in the range of 1.3 to 2.5 hours and more preferably 1.5 to 2.4 hours.
• Examples of the reaction product of the telomerization reaction in which butadiene and water are reacted in a carbon dioxide atmosphere include, in addition to 2,7-octadien-1-ol which is the target product, 1,7-octadien-3-ol, 1,3,7-octatriene, vinylcyclohexene, and 2,6-octadien-1-ol which has been found to be produced in a non-negligible amount.
• the molar ratio of the amount of 2,6-octadien-1-ol produced to the amount of 2,7-octadien-1-ol produced is preferably controlled in the range of 0.01% to 2.0%, more preferably controlled in the range of 0.01% to 1.5%, and still more preferably controlled in the range of 0.01% to 1.0%.
• the molar ratio of the total of the amounts of 1,3,7-octatriene and 1,7-octadien-3-ol produced to the amount of 2,7-octadien-1-ol produced is preferably controlled in the range of 1.0% to 20.0%, more preferably controlled in the range of 1.0% to 15.0%, and still more preferably controlled in the range of 1.0% to 10.0%.
• a catalyst component composed of a tertiary phosphorus compound and a palladium compound is separated and recovered from the reaction mixture liquid by a distillation method, an extraction method, or the like.
• the extraction method is carried out, for example, by carrying out the telomerization reaction and then subjecting the reaction mixture liquid to an extraction operation using a solvent immiscible with the reaction solvent as an extractant.
• the catalyst component can be separated as a raffinate component into a phase containing water and sulfolane.
• the organic phase obtained by the extraction operation contains butadiene, 2,7-octadien-1-ol, other by-products, amine compounds, and optionally carbon dioxide.
• Carbon dioxide and butadiene are removed by flashing the organic phase, and if necessary, at least a part of the removed carbon dioxide and butadiene is again fed to the telomerization reactor as a component of the raw material mixture liquid and cyclically reused.
• the amine compound, 2,7-octadien-1-ol, other by-products, and the like can be separated by distillation.
• the separated amine compound may be reused in the telomerization reaction.
• 2,7-octadien-1-ol may be separated by extracting at least a part of the reaction mixture liquid with an extractant.
• the extractant that can be used is not particularly limited, and examples thereof include a saturated aliphatic hydrocarbon, a monoolefinic hydrocarbon, and an alicyclic hydrocarbon, which have a boiling point lower than that of 2,7-octadien-1-ol.
• the extractant include saturated aliphatic hydrocarbons such as n-butane, isobutane, n-pentane, n-hexane, n-heptane, n-octane, and isooctane; monoolefinic hydrocarbons such as butene and isooctane; and alicyclic hydrocarbons such as cyclohexane, cyclohexene, and methylcyclohexane.
• saturated aliphatic hydrocarbons such as n-butane, isobutane, n-pentane, n-hexane, n-heptane, n-octane, and isooctane
• monoolefinic hydrocarbons such as butene and isooctane
• alicyclic hydrocarbons such as cyclohexane, cyclohexene, and methylcyclohexane.
• n-hexane is preferable.
• a mixture of hydrocarbons such as butane, butene, and isobutene contained in the C4 fraction as the butadiene source can also be used.
• the extractant is preferably used in an amount within a range of 0.3 to 3.0 in terms of a volume ratio with respect to the reaction mixture liquid.
• the raffinate layer (aqueous solution layer) containing the catalyst component is cyclically reused in the synthesis of 2,7-octadien-1-ol. If desired, a part of the raffinate layer may be taken out, subjected to a catalyst activation treatment, and then recycled to the above synthesis.
• an industrially general-purpose stirring type extraction tower, an RDC type extraction tower, a perforated plate tower, or the like can be applied.
• the extraction operation is carried out in a continuous manner by providing a standing tank sufficient for phase separation.
• the 2,7-octadien-1-ol is optionally purified from the extraction layer by conventional separation means such as distillation.
• the fraction containing 2,7-octadien-1-ol, which is the target product, as a main component can be purified by distillation under reduced pressure.
• the distillation temperature of the fraction containing 2,7-octadien-1-ol as a main component can be appropriately selected depending on the pressure in the distillation system, and is preferably 200° C. or lower, and more preferably 140° C. or lower, because the reaction of 2,7-octadien-1-ol to 1,3,7-octatriene or the like proceeds when the fraction is heated to around 200° C. in the presence of a trace amount of a palladium catalyst.
• the conversion rate of butadiene was calculated by Equation 1 below.
• the unit of each amount in the equation is mol.
• the calculation results are shown in Table 1.
• the “amount of butadiene in the reaction liquid” in Equation 1 means the “amount of butadiene in the reaction mixture liquid”
• the “amount of charged butadiene” means the “amount of butadiene in the raw material mixture liquid”.
• Butadiene ⁇ conversion ⁇ rate ⁇ ( % ) ( Equation ⁇ 1 ) 100 ⁇ [ 1 - ( Amount ⁇ of ⁇ butadiene ⁇ in ⁇ the ⁇ reaction ⁇ liquid ) / ( Amount ⁇ of ⁇ charged ⁇ butadiene ) ]
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 59 mol %, and the component composition of the product in the reaction mixture liquid was 88 mol % of 2,7-octadien-1-ol (2,7-ODA), 0.4 mol % of 2,6-octadien-1-ol (2,6-ODA), 2.3 mol % of 1,3,7-octatriene (OCT), and 5.0 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 51 mol %, and the component composition of the product in the reaction mixture liquid was 90 mol % of 2,7-octadien-1-ol (2,7-ODA), 0.5 mol % of 2,6-octadien-1-ol (2,6-ODA), 3.1 mol % of 1,3,7-octatriene (OCT), and 4.1 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 52 mol %, and the component composition of the product in the reaction mixture liquid was 89 mol % of 2,7-octadien-1-ol (2,7-ODA), 0.5 mol % of 2,6-octadien-1-ol (2,6-ODA), 2.3 mol % of 1,3,7-octatriene (OCT), and 4.5 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 50 mol %, and the component composition of the product in the reaction mixture liquid was 91 mol % of 2,7-octadien-1-ol (2,7-ODA), 0.6 mol % of 2,6-octadien-1-ol (2,6-ODA), 1.9 mol % of 1,3,7-octatriene (OCT), and 3.8 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 53 mol %, and the component composition of the product in the reaction mixture liquid was 91 mol % of 2,7-octadien-1-ol (2,7-ODA), 0.6 mol % of 2,6-octadien-1-ol (2,6-ODA), 2.4 mol % of 1,3,7-octatriene (OCT), and 4.1 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 54 mol %, and the component composition of the product in the reaction mixture liquid was 87 mol % of 2,7-octadien-1-ol (2,7-ODA), 2.0 mol % of 2,6-octadien-1-ol (2,6-ODA), 2.2 mol % of 1,3,7-octatriene (OCT), and 4.2 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• step (1) the reaction mixture liquid became a steady state.
• the butadiene conversion rate was 55 mol %, and the component composition of the product in the reaction mixture liquid was 86 mol % of 2,7-octadien-1-ol (2,7-ODA), 0.5 mol % of 2,6-octadien-1-ol (2,6-ODA), 4.5 mol % of 1,3,7-octatriene (OCT), and 4.1 mol % of 1,7-octadien-3-ol (IODA).
• the total pressure was adjusted to 1.4 MPaG with carbon dioxide.
• Examples 1 to 5 in which the residence time of the raw material mixture liquid in the telomerization reactor is within the range of 1.3 to 3.0 hours can improve the productivity of 2,7-octadien-1-ol while suppressing the production of 2,6-octadien-1-ol as a by-product, as compared to Comparative Examples 1 and 2 in which the residence time of the raw material mixture liquid in the telomerization reactor is outside the range of 1.3 to 3.0 hours.
• Example 4 From the comparison between Example 4 and Comparative Example 2 in Table 1, which have the same conditions except for the reaction liquid temperature and the residence time, it is found that in Example 4, the production of the by-product (OCT+IODA) can be reduced, and the productivity of 2,7-octadien-1-ol (2,7-ODA) is improved.
• the 2,7-octadien-1-ol obtained by the production method of the present invention can be derived into 7-octenal by isomerization using a copper-based catalyst, and thus is useful as a raw material of 7-octenal.
• 7-Octenal is a compound having a highly reactive terminal double bond and an aldehyde group, and is useful as a raw material for various industrial chemicals.
• 1,9-nonanedial is produced by subjecting 7-octenal to a hydroformylation reaction, and 1,9-nonanediamine useful as a raw material for a polymer monomer can be produced by further subjecting the 1,9-nonanedial to a reductive amination reaction.
• the 2,7-octadien-1-ol obtained by the production method of the present invention has an extremely low content of 2,6-octadien-1-ol, and therefore is also useful as a raw material for pharmaceuticals, agricultural chemicals, and the like.

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• 2023
  • 2023-02-21 EP EP23759974.1A patent/EP4484401A4/en active Pending
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